Research Papers

A Correlation for the Air-Side Heat Transfer Coefficient Assessment in Continuous Flat-Plate Finned Heat Exchangers

[+] Author and Article Information
Ali Hussain Tarrad

Assistant Professor
Jordanian Mottaa Company for Ice Cream,
P.O. Box 911728,
Amman 11191, Jordan
e-mail: dr.alitarrad@yahoo.com

Damiaa Saad Khudor

Mechanical Engineering Department,
College of Engineering,
Al-Mustansiriya University,
Baghdad 14150, Iraq
e-mail: damiaasaad@yahoo.com

1Corresponding author.

Contributed by the Heat Transfer Division of ASME for publication in the JOURNAL OF THERMAL SCIENCE AND ENGINEERING APPLICATIONS. Manuscript received August 24, 2014; final manuscript received December 11, 2014; published online January 28, 2015. Assoc. Editor: Zahid Ayub.

J. Thermal Sci. Eng. Appl 7(2), 021009 (Jun 01, 2015) (9 pages) Paper No: TSEA-14-1194; doi: 10.1115/1.4029459 History: Received August 24, 2014; Revised December 11, 2014; Online January 28, 2015

A simplified correlation for the air-side heat transfer coefficient exhibited from plate finned heat exchangers was accomplished. The development of the present formula was based on the implementation of the Buckingham-pi theorem. The physical dimensions of the plate fin parameters and tube geometry of the heat exchanger were incorporated in the correlation to reveal their effect on air-side heat transfer coefficient. It is intended to be used for air dry bulb and wet bulb temperatures in the range 16–40 °C and 13–20 °C through the tube banks, respectively. It is valid for transverse to longitudinal tube pitches ratio of XT/XL = 0.75 and 0.83. The air-side Reynolds number based on maximum flow velocity and equivalent tube diameter to be in the range of 2.2 × 103≤ Re ≤ 8.75 × 103. The total mean absolute errors of the predicted overall heat transfer coefficient and heat duty were 10% and 13%, respectively.

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Fig. 1

Continuous flat-plate fin tube [14,15]: (a) hexagonal and (b) rectangular

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Fig. 2

Typical tube shape of commercially available air cooled heat exchangers: (a) elliptical, (b) slot, (c) rounded rectangular, and (d) circular

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Fig. 3

Experimental setup [8]

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Fig. 4

The heat exchanger specifications used in the present work [8]: (a) staggered tube arrangement single-pass slot tube bank and (b) in-line tube arrangement multipasses circular tube bank

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Fig. 5

(a) A comparison between experimental and predicted air-side Nusselt number by the present correlation and (b) a comparison of the simplified air-side Nusselt number with that of experimental data

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Fig. 6

The accuracy limit for the experimental and predicted air-side heat transfer coefficient by the present work

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Fig. 7

A comparison of the predicted overall heat transfer coefficient and that of experimental data

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Fig. 8

Heat duty comparison between the present work prediction and experimental data

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Fig. 9

A comparison between the experimental air-side heat transfer coefficient of Tarrad et al. [8] with that of McQuiston and Parker [10]

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Fig. 10

A comparison for the present work prediction with that of McQuiston and Parker [10]: (a) overall heat transfer coefficient and (b) heat duty




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